System and method for selective catalytic reduction of nitrogen oxides in combustion exhaust gases

ABSTRACT

A multi-stage selective catalytic reduction (SCR) unit ( 32 ) provides efficient reduction of NOx and other pollutants from about 50-550° C. in a power plant ( 19 ). Hydrogen ( 24 ) and ammonia ( 29 ) are variably supplied to the SCR unit depending on temperature. An upstream portion ( 34 ) of the SCR unit catalyzes NOx+NH 3  reactions above about 200° C. A downstream portion ( 36 ) catalyzes NOx+H 2  reactions below about 260° C., and catalyzes oxidation of NH 3 , CO, and VOCs with oxygen in the exhaust above about 200° C., efficiently removing NOx and other pollutants over a range of conditions with low slippage of NH 3 . An ammonia synthesis unit ( 28 ) may be connected to the SCR unit to provide NH 3  as needed, avoiding transport and storage of ammonia or urea at the site. A carbonaceous gasification plant ( 18 ) on site may supply hydrogen and nitrogen to the ammonia synthesis unit, and hydrogen to the SCR unit.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application claims benefit of the 31 May 2007 filing date of U.S.provisional application 60/932,466.

STATEMENT REGARDING FEDERALLY SPONSORED DEVELOPMENT

Development for this invention was supported in part by Contract No.DE-FC26-05NT42644, awarded by the United States Department of Energy.Accordingly, the United States Government may have certain rights inthis invention.

FIELD OF THE INVENTION

This invention relates to a system and a method for reduction ofnitrogen oxides (NOx) in combustion exhaust by selective catalyticreduction (SCR) with ammonia and hydrogen as reducing agents. Theinvention relates generally to the field of power generation, and moreparticularly to the control of atmospheric pollutants produced duringthe combustion of a fuel containing hydrogen to produce power, andspecifically to the catalytic treatment of exhaust gases from a gasturbine power generating station at a coal gasification plant.

BACKGROUND OF THE INVENTION

In order to reduce emissions of air pollutants, and especially NitrogenOxides (NOx) in the United States, the Environmental Protection Agency(EPA) is steadily tightening emissions standards for the powergeneration industry, including gas, oil, and coal-fired power plants. Aprogressive method to produce power is by gasification of coal and/orother carbonaceous materials, resulting in production of ahydrogen-containing fuel gas, followed by combustion of this fuel in agas turbine. This method allows effective production of power, andallows reduction of emissions of several air pollutants such as CO,volatile organic compounds (VOCs), etc. into the ambient air. However,combustion of hydrogen or hydrogen-containing fuel in a gas turbine athigh efficiency leads to a significant amount of NOx in the exhaustgases that must be removed.

Existing NOx reduction technologies include selective catalyticreduction (SCR) as an efficient way to reduce emissions of NOx to lowlevels. Various reducing agents can be used in SCR systems, includinghydrocarbons, hydrogen, ammonia, urea, etc. Ammonia is the mostefficient reducing agent at reducing NOx emissions to low levels. Ureaalso produces ammonia by its decomposition in the process of NOxreduction. However, ammonia has several disadvantages:

-   -   Ammonia is toxic, so its storage requires strong safety        measures. Accidental release of ammonia from a storage tank is a        hazard.    -   Ammonia slipping through the SCR process without reacting can        reach levels of 5-10 ppm in the final exhaust, which is harmful        to the environment.    -   Delivery of ammonia to a power generation station is hazardous.    -   Ammonia is not fully effective as a NOx reducing agent until the        temperature in the SCR reactor reaches about 260-300° C. or        higher, so NOx is not effectively reduced by ammonia during        start-up cycles of power generation units, when exhaust        temperatures are lower.

BRIEF DESCRIPTION OF THE DRAWINGS

The invention is explained in the following description in view of thedrawings that show:

FIG. 1 is a schematic view of a system for selective catalytic reductionof NOx using ammonia and hydrogen produced on-site at a power generationplant using fuel gases from coal gasification.

FIG. 2 is a schematic view of an SCR unit according to aspects of theinvention.

FIG. 3 schematically illustrates relative efficiencies of two stages ofcatalytic operation of the present SCR unit depending on the exhausttemperature.

FIG. 4 illustrates a method of the invention.

DETAILED DESCRIPTION OF THE INVENTION

The present invention provides a system and method for reducing NOx inexhaust gases, especially in those produced by combustion of hydrogen ora hydrogen-containing fuel such as a fuel gas from coal gasification.The invention provides high NOx reduction efficiencies over a wide rangeof operating temperatures, including start-up temperatures, and withouta need for ammonia or urea delivery and storage. It is especially usefulfor power plants that use combustion devices such as gas turbines.

FIG. 1 illustrates a NOx removal system 20 with an ammonia synthesisunit 28 and a multi-stage selective catalytic reduction unit (SCR) 32.The SCR unit 32 can utilize both hydrogen 24 and ammonia 29 as reducingagents. Nitrogen 22 and hydrogen 23 may be supplied to the ammoniasynthesis unit 28 from a plant 18 that gasifies a carbonaceous materialsuch as coal 17. The nitrogen 22 and hydrogen 23 may be mixed 26 andthen converted to ammonia 29 in the ammonia synthesis unit 28. Anyammonia synthesis process may be used, such as the Haber process. TheSCR unit 32 receives combustion exhaust 30 from a power plant gasturbine 19, injects 33 the reducing agent(s) 24, 29 into the exhaust 30,and reduces the concentration of NOx prior to release of the exhaust 38to the atmosphere.

As shown in FIG. 2, the SCR unit 32 may incorporate an ammonia/hydrogeninjection grid 33 that injects and mixes the reducing agent(s) 24, 29into the combustion exhaust 30. A multifunction catalytic element 34, 36is located downstream of the injection grid 33. An upstream catalystportion 34 of the catalytic element comprises a substrate of a suitablematerial such as zeolites or metal oxides impregnated and/or coated witha first catalytic material that promotes reactions between nitrogenoxides and ammonia to produce nitrogen and water. A downstream catalystportion 36 may comprise the same substrate and the same catalyticmaterial or a similarly-acting catalytic material as the upstreamcatalyst portion 34, plus one or more catalytic metals of the platinumgroup that, depending upon the temperatures of the exhaust, promoteoxidizing reactions or reaction between nitrogen oxides and hydrogen.

The upstream catalyst portion 34 of the SCR unit 32 may comprise 10 to90% of the total catalyst bed volume, preferably 40 to 60%. Embodimentsof such catalytic materials are described in commonly assigned U.S.patent application Ser. No. 11/282,036, published on 17 May 2007 asPublication US 2007/0110643 A1 and incorporated herein by reference inits entirety. The downstream catalyst portion 36 of the catalyticelement has an active component of platinum group metals. Pd ispreferred over Pt because Pd exhibits better catalytic selectivity toyield N₂ over NOx as a product of NOx+NH₃ reactions above 200° C. Pdalso exhibits better catalytic selectively to yield N₂ over NOx as aproduct of NOx+H₂ reactions below 200° C.

FIG. 3 illustrates relative reaction efficiencies of NOx+hydrogen andNOx+ammonia, depending on temperature. At temperatures from about 100°C. to about 260° C. the downstream catalyst portion 36 promotes hydrogenas a reducing agent. Hydrogen reacts with NOx to produce nitrogen andwater via the catalytic effect of a metal or metals of the platinumgroup. At temperatures above about 260° C. the oxidizing catalyticfunction of metals of the platinum group in the downstream catalystportion 36 increases. As a result, hydrogen is oxidized by oxygen in theexhaust gases into water at a much higher rate. This reduces thehydrogen available to react with nitrogen oxides.

As temperatures rise above about 200° C., a transition to ammonia as areducing agent can be made by utilizing the upstream catalyst portion 34of the catalytic device 32. Reduction reactions between NOx and ammoniacontinue in the downstream catalyst portion 36 via the same or asimilar-acting catalyst as in the upstream catalyst portion, but thesereactions occur at a lower rate due to increased activity of theoxidizing catalytic metals of the platinum group that convert ammonia tonitrogen and water. Simultaneously with oxidizing of ammonia, any carbonmonoxide and hydrocarbons that may present in the exhaust gases areoxidized to nitrogen, CO₂, and water. The reduction and oxidizingactivity ratio in the downstream catalyst portion 36 depends on theactivity of oxidizing catalytic metals, operating parameters, andinitial concentrations of the impurities in the combustion exhaustgases.

During a start-up period of a power generation unit such as a gasturbine the temperature of the SCR catalyst is not suitable toefficiently provide the reaction between ammonia and NOx but it is highenough to promote reaction between hydrogen and NOx within thedownstream catalyst portion 36. During start-up, a small portion 24 ofthe hydrogen fuel flow to the power generation unit can be directed intothe SCR unit 32 to serve as reducing agent. As the temperature of theSCR increases, the reaction between hydrogen and NOx becomes lessfavorable, and part of the hydrogen flow 25 is directed into the ammoniasynthesis unit 28, where hydrogen and nitrogen react to produce ammoniathat is forwarded 29 into the SCR unit 32 to complete reduction of NOx.

The amounts and proportions of hydrogen and ammonia supplied to the SCRunit may be automatically controlled 40 depending on the temperature andchemical composition of the exhaust gas 30. Sensors 42 can providetemperature, chemistry, and volume information to the process controller40 to control mixing valves 26, 44 and other process controls in thesystem for this purpose When the temperature of the SCR unit 32 is toolow for effective ammonia-NOx reaction, most or all of the hydrogen flow23, 24 may be routed to the SCR unit 32, and little or no ammonia may begenerated. When the temperature of the SCR unit 32 is in an optimalrange for ammonia-NOx reaction, most or all of the hydrogen flow 23, 25may be routed to the ammonia synthesis unit 28 to supply enough ammoniafor the reaction. Excess ammonia is destroyed in the downstream catalystportion 36 of the catalytic device 32, so only traces of ammonia slipinto the ambient air.

Thus, the SCR unit 32 operates as a hydrogen or ammonia SCR depending onthe temperature of the SCR unit. This provides low NOx emissionsthroughout a full range of operating and load conditions of a generationpower unit, including effective reduction of NOx during start-up. Thisis impossible with a conventional ammonia SCR system because thestart-up temperature is too low to facilitate reactions between NOx andNH₃. The system 20 may automatically adjust ammonia flow depending onNOx concentrations measured upstream of the SCR unit 32 by varying theamount of hydrogen 25 directed into the ammonia synthesis unit 28. TheSCR unit can be designed to operate effectively between 50 and 550° C.,or preferably between 105 and 350° C. It can be designed to operate at agas hourly space velocity (GHSV) of 1,000-200,000 volumes per hour, orpreferably 10,000-40,000 volumes per hour, with an exhaust streamcontaining between 5 and 21% oxygen.

FIG. 4 illustrates aspects of the invention as a method 60 of removingnitrogen oxides (NOx) from combustion exhaust, comprising: synthesizing62 a fuel gas from a carbonaceous material, such as coal; separating 64nitrogen from the air; separating 66 some of the hydrogen from the fuelgas; supplying 68 fuel gas and air with reduced nitrogen content to apower plant; supplying 70 hydrogen and nitrogen from the separationprocesses to an ammonia synthesizer; supplying 72 hydrogen from thehydrogen separation process to a multi-stage SCR unit; supplying 74ammonia to the multi-stage SCR unit from the ammonia synthesizer;sensing 76 the temperature, chemistry, and flow rate of the power plantcombustion exhaust, supplying 78 the exhaust to the SCR unit;controlling 80 the hydrogen and ammonia proportions and amounts suppliedto the SCR unit and to the ammonia synthesizer depending on thetemperature, chemistry, and flow rate of the exhaust; catalyzing 82ammonia+NOx in the exhaust at temperatures above about 200° C.;catalyzing 84 hydrogen+NOx in the exhaust at temperatures up to about260° C.; oxidizing 86 ammonia, CO, and VOCs in the exhaust with oxygenin the exhaust at temperatures above about 200° C.; and releasing 88cleaned exhaust into the environment.

An alternative configuration of the catalytic element 34, 36 involvesimpregnating the upstream catalyst portion 34 of the catalyst bed with asmall amount of platinum group metals, such as less than 1% of aplatinum metal such as Ru, Rh, Pd, Os, Ir, or Pt, or less than 1% basemetal such as W, Zr, Fe, Ni, Cu, Pb, or Zn. The downstream catalystportion 36 remains the same as described previously. This configurationenhances the hydrogen activity as a reducing agent, but requires thatthe process be operated at a slightly greater NH₃ to NO_(x) ratio in theammonia SCR mode, since a small portion of the ammonia will be oxidized.

While various embodiments of the present invention have been shown anddescribed herein, it will be obvious that such embodiments are providedby way of example only. Numerous variations, changes and substitutionsmay be made without departing from the invention herein. Accordingly, itis intended that the invention be limited only by the spirit and scopeof the appended claims.

1. A system for removal of nitrogen oxides (NOx) from combustion exhaustproduced by an engine, the system comprising; a selective catalyticreduction (SCR) unit that reacts NOx in the exhaust with injectedhydrogen at exhaust temperatures below about 260° C. to produce nitrogenand water, and reacts NOx in the exhaust with injected ammonia attemperatures above about 200° C. to produce nitrogen and water, andoxidizes carbon monoxide, hydrocarbons, and ammonia in the exhaust atexhaust temperatures above about 200° C. to produce nitrogen, CO₂, andwater; whereby pollutants are removed from the combustion exhaust over arange of temperatures produced during start-up and operation of theengine.
 2. The system of claim 1, further comprising an ammoniasynthesis unit installed on a site with the SCR unit, and connectedthereto by an ammonia communication line, wherein the ammonia synthesisunit produces ammonia for the SCR unit as needed, whereby a need fordelivery and storage of ammonia on the site is eliminated.
 3. The systemof claim 2, wherein the SCR unit is installed at an electrical powergeneration plant fueled by a hydrogen-containing fuel gas produced by anon-site carbonaceous gasification plant that also produces and suppliesnitrogen and the hydrogen to the ammonia synthesis unit.
 4. The systemof claim 2, further comprising sensors that detect a temperature of thecombustion exhaust and/or the SCR unit, and detect a flow volume andchemistry of the combustion exhaust, and input these parameters to acontroller that automatically adjusts proportions and amounts of thehydrogen and the ammonia supplied to the SCR unit depending on operatingconditions.
 5. The system of claim 3, wherein the hydrogen isproportioned between a first and a second flow of the hydrogen, thefirst flow routed to an injector in the SCR unit that mixes the hydrogeninto the combustion gas, and the second flow routed to the ammoniasynthesis unit that supplies the ammonia to the injector; wherein whenthe temperature of the combustion exhaust is too low for effectiveammonia-NOx reactions, the first hydrogen flow is increased relative tothe second hydrogen flow, and when the temperature of the combustionexhaust is in an optimal range for ammonia-NOx reaction, the secondhydrogen flow is increased relative to the first hydrogen flow.
 6. Thesystem of claim 5, wherein the SCR unit comprises: an upstream catalystportion that is located downstream from the injector, the upstreamcatalyst portion comprising a substrate impregnated and/or coated with afirst catalytic material that promotes a reaction between NOx in thecombustion exhaust and ammonia at temperatures above about 200° C. toproduce nitrogen and water; a downstream catalyst portion that islocated downstream from the upstream catalyst portion, the downstreamcatalyst portion comprising a substrate impregnated and/or coated withthe first catalytic material or a similarly-acting catalytic material,and wherein the downstream catalyst portion substrate is alsoimpregnated and/or coated with a metal of the platinum group thatpromotes oxidizing reactions at temperatures above 200° C., and areaction between NOx in the combustion exhaust and hydrogen attemperatures below about 260° C. to produce nitrogen and water.
 7. Thesystem of claim 6, wherein the upstream catalyst portion furthercomprises less than 1% by volume of a metal of the platinum group orless than 1% of a base metal that catalyzes hydrogen as a NOx reducingagent.
 8. A system for removal of nitrogen oxides (NOx) from combustionexhaust, comprising: an injection device that mixes hydrogen and ammoniainto the combustion exhaust in varying proportions depending on atemperature of the combustion exhaust; an upstream catalyst portion thatis located downstream from the injection device, the upstream catalystportion comprising a substrate impregnated and/or coated with acatalytic material that promotes a reaction between NOx in thecombustion exhaust and ammonia at temperatures above about 200° C. toproduce nitrogen and water; a downstream catalyst portion that islocated downstream from the upstream catalyst portion, the downstreamcatalyst portion comprising a substrate impregnated and/or coated withthe catalytic material or a similarly-acting catalytic material, andwherein the downstream catalyst portion substrate is also impregnatedand/or coated with a metal of the platinum group that promotes oxidizingreactions at temperatures above 200° C., and a reaction between NOx inthe combustion exhaust and hydrogen at temperatures below about 260° C.to produce nitrogen and water.
 9. The system of claim 8, wherein theupstream catalyst portion further comprises less than 1% by volume of ametal of the platinum group or less than 1% of a base metal thatenhances hydrogen as a reducing agent.
 10. The system of claim 8,further comprising an ammonia synthesis unit connected to the injectiondevice by an ammonia communication line, wherein the ammonia synthesisunit produces ammonia for the injection device as needed.
 11. The systemof claim 10, installed at an electrical power generation plant fueled bya hydrogen-containing fuel gas produced by a fuel synthesis plant thatalso produces and supplies nitrogen and hydrogen for and to the ammoniasynthesis unit.
 12. A method of removing nitrogen oxides (NOx) fromcombustion exhaust, comprising: synthesizing a fuel gas containinghydrogen by gasification of a carbonaceous material; separating some ofthe hydrogen from the fuel gas; mixing at least some of the separatedhydrogen into the combustion exhaust; catalyzing a reaction between NOxin the combustion exhaust and the hydrogen that removes NOx from theexhaust at temperatures up to about 260° C.; separating nitrogen fromair; synthesizing ammonia from at least some of the separated hydrogenand nitrogen; mixing the ammonia into the combustion exhaust; catalyzinga reaction between NOx in the combustion exhaust and the ammonia thatremoves NOx from the exhaust at exhaust temperatures above about 200°C.; and catalyzing oxidation reactions of ammonia, carbon monoxide, andvolatile organic compounds in the exhaust downstream of the NOx-ammoniareaction at exhaust temperatures above about 200° C.
 13. The method ofclaim 12, further comprising: sensing a temperature of the combustionexhaust; sensing a NOx concentration in the combustion exhaust; andproportioning the separated hydrogen between a first and a second flowof the hydrogen, the first hydrogen flow routed to an injector thatmixes the hydrogen into the combustion gas, and the second hydrogen flowrouted to an ammonia synthesis unit that supplies the ammonia to theinjector; wherein when the temperature of the combustion exhaust is toolow for effective ammonia-NOx reaction, the first hydrogen flow isincreased relative to the second hydrogen flow, and when the temperatureof the combustion exhaust is in an optimal range for ammonia-NOxreaction, the second hydrogen flow is increased relative to the firsthydrogen flow.
 14. The method of claim 12, further comprising: sensing atemperature parameter of the combustion exhaust; sensing a NOxconcentration parameter in the combustion exhaust; sensing a flow volumeparameter of the combustion exhaust; inputting the sensed parameters toa controller that automatically adjusts proportions and amounts of thehydrogen and the ammonia mixed into the combustion exhaust depending onoperating conditions, wherein when the temperature of the combustionexhaust is too low for effective ammonia-NOx reaction, proportionallymore hydrogen and less ammonia is mixed into the combustion exhaust, andwhen the temperature of the combustion exhaust is in an optimal rangefor ammonia-NOx reaction, proportionally more ammonia and less hydrogenis mixed into the combustion exhaust.